CN1556847A - Methods for treating deodorizer distillate - Google Patents
Methods for treating deodorizer distillate Download PDFInfo
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- CN1556847A CN1556847A CNA028186214A CN02818621A CN1556847A CN 1556847 A CN1556847 A CN 1556847A CN A028186214 A CNA028186214 A CN A028186214A CN 02818621 A CN02818621 A CN 02818621A CN 1556847 A CN1556847 A CN 1556847A
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- enrichment region
- evaporated fraction
- enriched material
- fill area
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07J—STEROIDS
- C07J9/00—Normal steroids containing carbon, hydrogen, halogen or oxygen substituted in position 17 beta by a chain of more than two carbon atoms, e.g. cholane, cholestane, coprostane
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B13/00—Recovery of fats, fatty oils or fatty acids from waste materials
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
Abstract
This invention relates to methods for treating distillates obtained during the process of deodorizing various oils. More particularly, this invention relates to methods for recovering fatty acids, tocopherols, and sterols from a distillate obtained from the doedorizing of various oils.
Description
Technical field
The present invention relates to handle the method for carrying out the cut that obtains in the de-odorised process by different oil.More specifically, the present invention relates to from different oil carries out cut that deodorizing obtains, reclaim the method for lipid acid, tocopherol and sterol.
Background technology
By the plant and animal oil that obtains of deriving is the valuable source of lipid acid, tocopherol and sterol.But in refining this type of oily process, according to selected process for extracting, a large amount of specific examples of such components, particularly tocopherol are lost in different intermediate by-products and waste streams with sterol, comprise acidified soapstock, in reodorant cut or the two.Therefore, proposed a large amount of methods and be used for reclaiming lipid acid, tocopherol and sterol from different refinement intermediate products, described refinement intermediate product is included in the reodorant cut as by product that the pyrogenic distillation step (being commonly referred to deodorizing) in the process of producing oil ﹠ fat obtains.
Produce oil ﹠ fat, the step that deodorizing is normally last by the plant and animal source.Vegetables oil such as soya-bean oil contain the volatile impunty that can bring disagreeable aroma and flavor usually.For producing edible oil, need remove these volatile compounds usually.Deodorizing comprises stripping (stripping) process usually, wherein steam and oil in rectifier unit, contact, this device with low pressure be enough to make undesirable volatile impunty under the temperature of evaporating under the operated pressure, to move.Be commonly referred to vacuum-this method of steam de-odorised depend on oil and undesirable impurity between the volatility difference, stripping is sloughed more relatively volatile undesirable impurity from less relatively volatile oil.In common vacuum-steam deodorizing method, vegetables oil is introduced in the rectifier unit, and this device has the dish of a plurality of perpendicular separations, is commonly referred to stripping dish (stripping trays).In each stripping dish, inject vegetables oil entrainment with steam undesirable volatile impunty.Usually collect and concentrate steam that interosculates and the rectifying steam of carrying secretly, formation can further be handled or process to be reclaimed the cut of valuable raw material.
The main composition of reodorant cut is lipid acid, tocopherol and sterol, and according to the source and the oily refining step that is experienced before deodorizing of oil, they exist with different relative quantities.The reodorant cut itself has certain commercial value.But, when the reodorant cut is separated into the part that is rich in lipid acid and is rich in the part of sterol and tocopherol, have higher value.
Isolated lipid acid can be used for some non-food product purposes from the reodorant cut, in particular as the liquid agent of Yelkin TTS.This type of lipid acid also can be used as the precursor of a large amount of molecule synthesis methods.Usually the fatty acid part of reodorant cut comprises C
10-C
22Saturated and unsaturated fatty acids.Particularly, soybean reodorant cut contains the lipid acid of the 50wt% that has an appointment.
The reodorant cut also contains sterol, and it is to produce hormonal valuable precursor.Stigmasterol is used to produce Progesterone and corticoid.Sitosterol is used to produce oestrogenic hormon, contraceptive bian, diuretic(s) and male hormone.Particularly, soybean reodorant cut contains the sterol of the 10-18wt% that has an appointment altogether, and wherein about 50% is Sitosterol, and about 20% is Stigmasterol, and about 20% is campesterol, and about 10% is other a small amount of sterol.
The last main ingredient of reodorant cut is a tocopherol.Tocopherol is valuable antioxidant, helps to prevent and treat oxidation and rotten.Tocopherol also can be used for producing vitamin-E.The cut that obtains from the soybean oil deodorizing contains usually and proportionally is about 15: 5: 30: 50 α, beta, gamma and methyltocol mixture of isomers.Alpha-tocopherol has maximum vitamin-E biological activity.Other tocopherol has more weak vitamin-E activity, but has stronger anti-oxidant activity.Zui Da vitamin-E activity can be converted into non-alpha-tocopherol the form of alpha-tocopherol by known technology as methylating if desired.
In the past, from reodorant cut and relative mixture, reclaim tocopherol and sterol and be proved to be complicated and costliness.The boiling point that a difficulty relevant with separate one or more cuts that are rich in lipid acid, tocopherol and/or sterol from the reodorant cut is sterol and tocopherol is roughly in identical scope.Another difficulty is, if reodorant cut long time of processing under the temperature of sterol and tocopherol evaporation, thermal destruction can take place the reodorant cut, and such temperature condition can cause that lipid acid is converted into undesirable trans-isomerism form.
Proposed a large amount of method and handled the reodorant cut to separate and to reclaim one or more components.In a lot of these methods, first basic step is to make lipid acid carry out esterification and saponification reaction.For example, the US patent No. 3,153,055 has disclosed a kind of method of separating sterol and tocopherol from the reodorant cut, this method by lipid acid and monohydroxy-alcohol esterification under strong acid condition carry out.Unite then and utilize polarity and non-polar solvent segmentation from the esterification products mixture (fractionally) to extract sterol and tocopherol.
In another kind of esterification process, the US patent No. 5,487,817 has disclosed sterol and fatty acid esterification, rectifying gained mixture then, the cut that obtains containing the resistates of sterol ester and contain tocopherol.Sterol ester is divided under acidic conditions, from this resistates, separate sterol.
The US patent No. 2,349,270 discloses available lime soap processing reodorant cut and has made fatty acid saponification, uses the unsaponified part of acetone extract (tocopherol and sterol) then, and wherein saponification resultant is insoluble.Wash then and concentrated extract, for example by solvent distillation, crystallisation by cooling sterol then, it can be filtered and remove, and stays highly purified tocopherol part.The fatty acid soaps that this method forms can be converted into free fatty acids by acidifying.
Extraction separating method also can be used for handling the reodorant cut to separate one or more components.For example, the US patent No. 5,138,075 has been described the method that reclaims tocopherol from the reodorant cut, comprise this cut is contacted under high temperature and high pressure with liquid water to have the residual oil phase liquid stream of higher concentration tocopherol and have the extract phase liquid stream of higher concentration lipid acid with preparation.Cool off Raffinate stream and extract liquid then and flow to organic constituent and the immiscible temperature of liquid water, remove and anhydrate, the part that obtains being rich in the part of tocopherol respectively and be rich in lipid acid.
But do not have gratifying in the above-mentioned method of from the reodorant cut, separating one or more components.The several different methods that comprises esterif iotacation step and saponification step is brought the processed complex problem, and needs the subsequent process steps behind the use strong inorganic acid to make ester or soap be converted into free sterol and free fatty acids respectively.Mineral acid is danger close in operation, can cause cut variable color or other degraded.Need the method for extraction step very expensive, and can produce the residual solvent contamination of heavy.
The method of separating one or more components from the reodorant cut of previously known needs time-consuming and expensive procedure of processing usually.Therefore, need seek the method for further improved processing reodorant cut.The present invention relates to have improving one's methods of the advantage that is better than previous disclosed method.Method of the present invention directly and obtain being rich in the cut of lipid acid simply from the cut of evaporation.Method of the present invention has also obtained being rich in the cut of sterol and tocopherol, and its available diverse ways is further handled to separate sterol part and tocopherol part.
Summary of the invention
One aspect of the present invention relates to the method for separating one or more components from the evaporated fraction that different oily deodorizing obtains.
Another aspect of the present invention relates to and prepare the method that is rich in free fatty acid mixture from the cut that different oily deodorizing obtains.
Another aspect of the present invention relates to the method for preparing the mixture that is rich in sterol and tocopherol from the cut that different oily deodorizing obtains.
One embodiment of the invention are methods of separated portion from evaporated fraction, may further comprise the steps: the evaporated fraction that will contain sterol, tocopherol and lipid acid is introduced first enrichment region of upgrading unit, this upgrading unit has at least two enrichment regions and operates under the pressure less than 10mm Hg, and this first enrichment region is operated under about 330-450 temperature; In the first part of this first enrichment region concentration and evaporation cut, obtain being rich in first enriched material of sterol and tocopherol, stay the remainder of evaporated fraction; The remainder of this evaporated fraction is introduced second enrichment region of upgrading unit, and this second enrichment region is operated under about 170 temperature range of about 100-; And, obtain being rich in second enriched material of lipid acid at the second section of the second enrichment region concentration and evaporation cut remainder, stay exhaust steam.
Another embodiment of the invention is the method for separated portion from evaporated fraction, may further comprise the steps: the evaporated fraction that will contain sterol, tocopherol and lipid acid is introduced first enrichment region of upgrading unit, this upgrading unit has at least two enrichment regions and operates under the pressure less than 10mm Hg, and this first enrichment region is operated under about 330-450 temperature; In the first part of this first enrichment region concentration and evaporation cut, obtain being rich in first enriched material of sterol and tocopherol, stay the remainder of evaporated fraction; The remainder of this evaporated fraction is introduced second enrichment region of upgrading unit, and this second enrichment region is operated under about 170 temperature range of about 100-; At the second section of the second enrichment region concentration and evaporation cut remainder, obtain being rich in second enriched material of lipid acid, stay exhaust steam; Reclaim this first enriched material; And reclaim this second enriched material.
Another embodiment of the present invention is the method for separated portion from evaporated fraction, may further comprise the steps: the evaporated fraction that will contain sterol, tocopherol and lipid acid is introduced first enrichment region of upgrading unit, this upgrading unit has at least two enrichment regions and operates under the pressure less than 10mm Hg, and this first enrichment region is operated under about 330-450 temperature; By making evaporated fraction flow through first fill area (packing), make the first part of evaporated fraction concentrate first enriched material that obtains being rich in sterol and tocopherol at this first enrichment region, stay the remainder of evaporated fraction, recirculation first enriched material that is maintained at about 380 in this first fill area place evaporated fraction and temperature contacts; The remainder of this evaporated fraction is introduced second enrichment region of upgrading unit, and this second enrichment region is operated under about 170 temperature range of about 100-; Repair by the remainder that makes evaporated fraction and to flow through second fill area, make the second section of evaporated fraction remainder concentrate second enriched material that obtains being rich in lipid acid at second enrichment region, stay exhaust steam, recirculation second enriched material that is maintained at about 135 in the remainder and the temperature of this second fill area place evaporated fraction contacts.
Another embodiment of the present invention is the method for separated portion from evaporated fraction, may further comprise the steps: the evaporated fraction that will contain sterol, tocopherol and lipid acid is introduced first enrichment region of upgrading unit, this upgrading unit has at least two enrichment regions and operates under the pressure less than 10mm Hg, and this first enrichment region is operated under about 330-450 temperature; By making evaporated fraction flow through first fill area, make the first part of evaporated fraction concentrate first enriched material that obtains being rich in sterol and tocopherol at this first enrichment region, stay the remainder of evaporated fraction, recirculation first enriched material that is maintained at about 380 in this first fill area place evaporated fraction and temperature contacts; The remainder of this evaporated fraction is introduced second enrichment region of upgrading unit, and this second enrichment region is operated under about 170 temperature range of about 100-; Flow through second fill area by the remainder that makes evaporated fraction, make the second section of evaporated fraction remainder concentrate second enriched material that obtains being rich in lipid acid at second enrichment region, stay exhaust steam, recirculation second enriched material that is maintained at about 135 in the remainder and the temperature of this second fill area place evaporated fraction contacts; Reclaim this first enriched material; And reclaim this second enriched material.
According to the following detailed description, these aspects of the present invention and others will become clear.
The detailed description of accompanying drawing
Fig. 1 is the side-view that is applicable to the washing tower of implementing the inventive method, has shown employed and/or the different steam that obtain and the flowing-path of enriched material logistics.
The description of preferred embodiment
Of the present invention improving one's methods is used for the evaporated fraction separated portion that obtains from different oily deodorizing.A lot of these type of cuts are applicable to the present invention, include but not limited to those evaporated fraction that obtain from following oily deodorizing: soya-bean oil, Semen Maydis oil, Oleum Gossypii semen, plam oil, peanut oil, rapeseed oil, Thistle oil, Trisun Oil R 80, sesame oil, Rice pollard oil, Oleum Cocois, rapeseed oil and composition thereof.The cut of particularly suitable is a soya-bean oil reodorant cut.
According to the type of oil and the refinement process before the deodorizing, the composition of reodorant cut has difference.The cut that obtains from the soya-bean oil deodorizing of alkali boiling contains the lipid acid of the 50wt% that has an appointment, the sterol of about 15wt% tocopherol and about 18wt% usually.The cut that obtains from the soya-bean oil deodorizing of physical refining contains lipid acid, the tocopherol of about 9wt% and the sterol of about 11wt% of the 70wt% that has an appointment usually.Disclosed as the US patent No. 6,172,248, the cut that the refining soya-bean oil deodorizing that is obtained by the organic acid purifying method obtains contains lipid acid, the tocopherol of about 12wt% and the sterol of about 14wt% of the 55wt% that has an appointment usually.Conc forms of any this type of deodorizing cut, this type of cut and composition thereof all is applicable to the present invention.This type of cut preferably provides with evaporated form so that the thermal destruction risk is reduced to minimum, becomes enriched material and postheating and further adds and man-hour thermal destruction can take place when cut can cool off.Usually, be about 300 °F from the cut temperature of reodorant, pressure is about 2-6mm Hg.
With first enrichment region 30 of evaporated fraction 20 introducing upgrading units 10, this upgrading unit 10 has at least two enrichment regions and operates under the pressure less than 100mm Hg.This upgrading unit 10 can be any equipment that can operate under low pressure and high temperature, has at least two enrichment regions.Preferably, this upgrading unit 10 is the washing towers that constitute or be suitable for comprising at least two enrichment regions.The available low pressure of source generation easily arbitrarily.Usually use steam injector system (steam jet ejector system).Three sections vacuum systems of the most preferred Nash-Kinema of being to use (three-stage vacuum system) or two sections vacuum systems are added vacuum pump.Using three sections injection systems will be the about 6mm Hg of about 4-in the vacuum that upgrading unit produces.Preferably, upgrading unit 10 is operated under the pressure less than about 6mm Hg.Most preferably, upgrading unit 10 is operated under the pressure less than about 4mm Hg.
Under working pressure, first enrichment region 30 is at the boiling point that is lower than tocopherol and sterol but be higher than under the temperature of boiling point of lipid acid and operate.Table 1 has been listed the boiling point of tocopherol and sterol under several low pressure.
Table 1
| Pressure (mm Hg) | The tocopherol boiling point (°F) | The sterol boiling point (°F) |
| ????1 | ????450 | ????470 |
| ????2 | ????470 | ????475 |
| ????3 | ????490 | ????505 |
| ????4 | ????500 | ????520 |
Under each listed pressure of table 1, the boiling point of lipid acid is lower than 200 °F.Usually, first enrichment region 30 is at about 330-450 temperature operation.Preferably, first enrichment region 30 is operated under about 405 temperature of about 355-.Most preferably, first enrichment region 30 is at about 390 temperature operation of about 370-.
In first enrichment region 30, the first part of evaporated fraction 20 concentrates first enriched material 40 that obtains being rich in sterol and tocopherol, and it can be recovered and sell makes a profit or reprocessing.Remaining not concentration and evaporation cut is called the remainder 50 of evaporated fraction herein, flows to second enrichment region 60 and is used for reprocessing.Usually, first enriched material 40 that obtains accounts for the 50wt% of evaporated fraction 20.First enriched material 40 contains the lipid acid of the 5wt% that has an appointment usually, the tocopherol of about 25wt% and the sterol of about 30wt%.Randomly, the fluid level controller that is positioned at first enrichment region, 30 bottoms is kept the constant volume of system's first enriched material 40, gets rid of the first unnecessary enriched material and it is sent to storage or is used for follow-up procedure of processing.
Usually, at least a portion of first enriched material 40 is passed through nozzle 90, enters first enrichment region 30 as mist that flows to adverse current or spraying recirculation with evaporated fraction, cools off by direct with contacting of evaporated fraction when evaporated fraction upwards flows.Randomly, evaporated fraction 20 flows through first fill area 100, make the part of evaporated fraction 20 take place to concentrate at first enrichment region 30, at these first fill area, 100 places, this evaporated fraction with by heat exchanger 120 circulation temperature maintenance is contacted at about 380 recirculation first enriched material 110.
The use of fill area has significantly improved first enriched material and the synergistic surface-area of evaporated fraction of recirculation.Fill area itself also provides extra cooling source, and this is because this fill area tends to obtain the temperature of first enriched material of recirculation.The type of fill area is selected based on factor well known in the art, comprises physical strength, erosion resistance, cost, capacity and efficient.Fill area can adopt the form of stainless steel grid or net, porcelain or porcelain ring or saddle (saddles) or other inert material that is fit to.Preferably, first fill area 100 comprises that a plurality of intervals are very near and is provided with the prionodont Stainless Steel Disc in a plurality of holes.The amount of the first used fill area 100 depends on the cross-sectional area of first enrichment region 30, maximum required pressure decline (pressuredrop), the flow velocity of evaporated fraction 20 and the transformation efficiency that needed evaporated fraction is converted into first enriched material.Usually, for first enrichment region 30 with 42 inch diameter circular cross sections, adopting vertical dimension is the entire cross section that about 15 inches first fill area, 100, the first fill areas 100 extend through first enrichment region 30 substantially.
The remainder 50 that flows out the evaporated fraction of first enrichment region 30 enters second enrichment region 60 of upgrading unit 10, and the second section simmer down to of evaporated fraction remainder 50 is rich in second enriched material 70 of lipid acid herein, stays exhaust steam 80.Second enrichment region 60 is being operated under the temperature that is lower than the lipid acid boiling point under this working pressure.Usually, second enrichment region 60 is operated under about 100-170 temperature, and preferably, second enrichment region 60 is operated under about 125-145 temperature.Most preferably, second enrichment region 60 is at about 140 temperature operation of about 130-.
In second enrichment region 60, the second section of evaporated fraction remainder 50 concentrate obtain being rich in lipid acid, recyclable and sell second enriched material 70 of profit.Remaining exhaust steam 80 flows to vacuum system.Usually, gained second enriched material 70 accounts for the 50wt% of original evaporated fraction 20.Second enriched material 70 contains the lipid acid of the 90wt% that has an appointment usually and has only the sterol and the tocopherol of trace.Randomly, the fluid level controller that is positioned at second enrichment region, 60 bottoms has kept the constant volume of system's second enriched material 70, gets rid of the second unnecessary enriched material and sends to storage.
Usually, at least a portion of second enriched material 70 is by nozzle 130, enter second enrichment region 60 as mist that flows to adverse current or spraying recirculation, when the evaporated fraction remainder upwards flows, cool off by direct with contacting of evaporated fraction remainder 50 with evaporated fraction remainder 50.Randomly, evaporated fraction remainder 50 flows through second fill area 140, make evaporated fraction remainder 50 take place to concentrate at second enrichment region 60, at these second fill area, 140 places, this evaporated fraction remainder 50 with by heat exchanger 160 circulation temperature maintenance is contacted at about 135 recirculation second enriched material 150.Second fill area 140 can adopt the form identical or different with first fill area 100.Preferably, second fill area 140 has identical materials and identical shape with first fill area 100.
After making second enriched material 70, available known method is reprocessed to separate sterol and/or tocopherol cut it.For example, because tocopherol is soluble in the lower aliphatic alcohols as methyl alcohol, and sterol is insoluble substantially in this type of alcohol when cooling, and second enriched material can wash and filter the filtrate that obtains containing the insoluble part of sterol and contain tocopherol in methyl alcohol, and methyl alcohol is removed in redistillation.Perhaps, second enriched material and adsorption solvent are merged, by basic anion exchange resin, tocopherol optionally is adsorbed on the resin then, and sterol passes through.The tocopherol that is adsorbed by wash-out mutually as acetate from this resin elution.
More than or all documents of quoting later on such as patent, journal of writings and textbook all be incorporated herein by reference in full.
Person of skill in the art will appreciate that and to improve the present invention and do not depart from aim of the present invention and scope.The present invention be will further specify with the following example, aim of the present invention and scope described particular step or composition will not be restricted to but should not be misinterpreted as.
Embodiment 1
The temperature that obtains from the soya-bean oil deodorizing of organic refinement is about 300 evaporated fraction and flows into first enrichment region of washing towers with 250,000 pounds of flow velocitys hourly, and this washing tower setting includes two enrichment regions and operates under the pressure of about 4mm Hg.The reodorant cut contains the lipid acid of the 50wt% that has an appointment, and the tocopherol of about 12wt%, the sterol of about 14wt% and about 24wt% comprise other component of oil.
That washing tower comprises is high 14 feet, the cylinder tower of 42 inches of diameters.High about 4 feet of first enrichment region comprises that vertical dimension is 15 inches a fill area.It is very near and be provided with the prionodont Stainless Steel Disc in a plurality of holes that fill area in first enrichment region contains a plurality of intervals.Nozzle extends into first enrichment region that is arranged on the fill area.Provide vacuum by three sections vacuum systems of Nash-kinema or vacuum pump to washing tower.
The first part that enters containing of first enrichment region and have an appointment the 50wt% evaporated fraction concentrates and forms first enriched material, and it contains the lipid acid of the 5wt% that has an appointment, the tocopherol of about 25wt% and the sterol of about 30wt%.The evaporated fraction that enters first enrichment region upwards circulation and with fill area and effusive and contact with the recirculation that flows to adverse current first enriched material of evaporated fraction from nozzle.Recirculation first enriched material flows and makes its temperature be maintained at about 380 °F by heat exchanger.First enriched material is not used in the part of recirculation and is discharged and send to storage continuously.
Do not have spissated part evaporated fraction at first enrichment region, this paper is called the remainder of evaporated fraction, upwards flows into second enrichment region.The size of second enrichment region and first enrichment region and appearance similar.The second section that contains the original evaporated fraction of 50wt% of having an appointment concentrates at second enrichment region and forms second enriched material, and it contains the lipid acid of the 90wt% that has an appointment, the tocopherol of about 4wt% and the sterol of about 6wt%.The steam that enters second enrichment region upwards flow through and with fill area and effusive and contact with recirculation second enriched material of the flow direction adverse current of evaporated fraction from nozzle.Recirculation second enriched material flows and makes temperature maintenance at about 135 °F by heat exchanger.Storage is discharged and sent to part second enriched material that is not used in recirculation continuously.
Lipid acid is chain length distribution as follows in second enriched material:
％C16:0????15-26
％C18:0????13-22
％C18:1????20-29
％C18:2????28-38
％C18:3????2-8
Embodiment 2
The temperature that the soya-bean oil deodorizing of refining from routine obtains is about 330 evaporated fraction and flows into first enrichment region of washing towers with 250,000 pounds of flow velocitys hourly, and this washing tower is set to include two enrichment regions and operates under the pressure of about 2.5mm Hg.The reodorant cut contains the lipid acid of the 45wt% that has an appointment, and the tocopherol of about 15wt%, the sterol of about 20wt% and about 20wt% comprise other component of oil.
That washing tower comprises is high 18 feet, the cylinder tower of 60 inches of diameters.High about 5 feet of first enrichment region comprises that vertical dimension is 24 inches a fill area.It is very near and the prionodont Stainless Steel Disc in a plurality of holes arranged that fill area in first enrichment region contains a plurality of intervals.Nozzle extends into first enrichment region that is arranged on the fill area.Provide vacuum by three sections vacuum systems of Nash-kinema or vacuum pump to washing tower.
The first part that enters containing of first enrichment region and have an appointment the 55wt% evaporated fraction concentrates and forms first enriched material, and it contains the lipid acid of the 3wt% that has an appointment, the tocopherol of about 30wt% and the sterol of about 35wt%.The evaporated fraction that enters first enrichment region upwards flow through and with fill area and mass flowing nozzle and contact with the recirculation that flows to adverse current first enriched material of evaporated fraction.Recirculation first enriched material flows and makes its temperature be maintained at about 380 °F by heat exchanger.First enriched material is not used in the part of recirculation and is discharged and send to storage continuously.
Do not have spissated part evaporated fraction at first enrichment region, this paper is called the remainder of evaporated fraction, upwards flows into second enrichment region.The size of second enrichment region and first enrichment region and appearance similar.The second section that contains the original evaporated fraction of 45wt% of having an appointment concentrates at second enrichment region and forms the lipid acid that contains the 95wt% that has an appointment, the tocopherol of about 2wt% and the sterol of about 3wt%.The steam that enters second enrichment region upwards flow through and with fill area and mass flowing nozzle, contact with recirculation second enriched material of evaporated fraction flow direction adverse current.Recirculation second enriched material flows and makes temperature maintenance at about 135 °F by heat exchanger.Storage is discharged and sent to part second enriched material that is not used in recirculation continuously.
The lipid acid of second enriched material chain length distribution as follows:
％C16:0????15-26
％C18:0????13-22
％C18:1????20-29
％C18:2????28-38
％C18:3????2-8
Now complete, clear, succinctly and exactly the present invention and manufacturing thereof and use mode of the present invention and method have been described, so that manufacturing that those skilled in the art can be correlated with and use.Although more than described the preferred embodiments of the invention, in the described scope of claims, can modify and change not departing from the present invention.For particularly pointing out and knowing statement theme of the present invention, following claims are summed up the application.
Claims (17)
1. the method for separated portion from evaporated fraction comprises:
(a) evaporated fraction that will contain sterol, tocopherol and lipid acid is introduced first enrichment region of upgrading unit, and this upgrading unit has at least two enrichment regions and operates under the pressure less than 10mmHg, and this first enrichment region is operated under about 330-450 temperature;
(b) in the first part of this first enrichment region concentration and evaporation cut, obtain being rich in first enriched material of sterol and tocopherol, stay the remainder of evaporated fraction;
(c) remainder of this evaporated fraction is introduced second enrichment region of upgrading unit, this second enrichment region is operated under about 170 temperature range of about 100-; And
(d) at the second section of this second enrichment region concentration and evaporation cut remainder, obtain being rich in second enriched material of lipid acid, stay exhaust steam.
2. the method for claim 1, wherein this first enrichment region is operated under about 355-405 temperature.
3. the method for claim 1, wherein this first enrichment region is operated under about 370-390 temperature.
4. the method for claim 1, wherein this second enrichment region is operated under about 125-145 temperature.
5. the method for claim 1, wherein this second enrichment region is operated under about 130-140 temperature.
6. the method for claim 1 also comprises step (e): reclaim this first enriched material.
7. the method for claim 1 also comprises step (e): reclaim this second enriched material.
8. method as claimed in claim 7 also comprises step (f): reclaim this second enriched material.
9. the method for claim 1, wherein the concentrated of step (b) is to be undertaken by making this evaporated fraction flow through first fill area, contacts at first about 380 enriched material with temperature maintenance in this this evaporated fraction of first fill area place.
10. method as claimed in claim 9, wherein, this first fill area comprises at interval very near and is provided with a plurality of Stainless Steel Discs in a plurality of holes.
11. the method for claim 1, wherein, the concentrated of step (d) is to flow through second fill area by the remainder that makes this evaporated fraction to carry out, and contacts at about 135 recirculation second enriched material with temperature maintenance at the remainder of this this evaporated fraction of second fill area place.
12. method as claimed in claim 11, wherein, this second fill area comprises at interval very near and is provided with a plurality of Stainless Steel Discs in a plurality of holes.
13. method as claimed in claim 9, wherein, the concentrated of step (d) is to flow through second fill area by the remainder that makes this evaporated fraction to carry out, and contacts at about 135 recirculation second enriched material with temperature maintenance at the remainder of this this evaporated fraction of second fill area place.
14. method as claimed in claim 13, wherein, this first fill area comprises at interval very near and is provided with a plurality of Stainless Steel Discs in a plurality of holes.
15. method as claimed in claim 13, wherein, this second fill area comprises at interval very near and is provided with a plurality of Stainless Steel Discs in a plurality of holes.
16. method as claimed in claim 14, wherein, this second fill area comprises at interval very near and is provided with a plurality of Stainless Steel Discs in a plurality of holes.
17. the method for claim 1, wherein this upgrading unit is a washing tower.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US09/946,810 US6750359B1 (en) | 2001-09-04 | 2001-09-04 | Methods for treating deodorizer distillate |
| US09/946,810 | 2001-09-04 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1556847A true CN1556847A (en) | 2004-12-22 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA028186214A Pending CN1556847A (en) | 2001-09-04 | 2002-08-29 | Methods for treating deodorizer distillate |
Country Status (11)
| Country | Link |
|---|---|
| US (1) | US6750359B1 (en) |
| EP (1) | EP1465968B1 (en) |
| JP (1) | JP2005501908A (en) |
| CN (1) | CN1556847A (en) |
| AR (1) | AR038659A1 (en) |
| AU (1) | AU2002336405A1 (en) |
| BR (1) | BR0212313A (en) |
| CA (1) | CA2459351C (en) |
| DE (1) | DE60216514D1 (en) |
| MX (1) | MXPA04002116A (en) |
| WO (1) | WO2003020860A2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101812373A (en) * | 2010-04-16 | 2010-08-25 | 南通市康桥油脂有限公司 | Method for producing fatty acid by continuous graded rectification |
| CN102311876A (en) * | 2011-08-16 | 2012-01-11 | 山东渤海实业股份有限公司 | Two-grade distillate capture method in plant oil deodorization processing and device thereof |
| CN103491793A (en) * | 2011-03-24 | 2014-01-01 | 荷兰洛德斯克罗科兰有限公司 | Process for fractionating a vegetable oil |
| CN104508100A (en) * | 2012-07-12 | 2015-04-08 | 阿尔法拉瓦尔股份有限公司 | Deacidification of fats and oils |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7597783B2 (en) | 2001-07-23 | 2009-10-06 | Cargill, Incorporated | Method and apparatus for processing vegetable oils |
| CA2477604A1 (en) | 2002-03-13 | 2003-09-25 | Signum Biosciences, Inc. | Modulation of protein methylation and phosphoprotein phosphate |
| CA2480011A1 (en) * | 2002-03-18 | 2003-12-04 | Sciperio, Inc. | Dentritic cell nodes |
| JP4186191B2 (en) * | 2003-06-05 | 2008-11-26 | 山栄化学株式会社 | Plant sterol ester-containing hair cosmetic feel improver |
| US7923041B2 (en) | 2005-02-03 | 2011-04-12 | Signum Biosciences, Inc. | Compositions and methods for enhancing cognitive function |
| US8221804B2 (en) | 2005-02-03 | 2012-07-17 | Signum Biosciences, Inc. | Compositions and methods for enhancing cognitive function |
| SE530258C2 (en) * | 2006-02-15 | 2008-04-15 | Alfa Laval Corp Ab | A process for refining fats and oils |
| EP2435545B1 (en) * | 2009-05-26 | 2017-06-28 | Cargill, Incorporated | Oil compositions |
| DE102010009579B4 (en) * | 2010-02-26 | 2013-07-25 | Lurgi Gmbh | Process for deodorizing cooking oil |
| RU2558364C2 (en) | 2011-04-14 | 2015-08-10 | Альфа Лаваль Корпорейт Аб | Method of autocatalytic ethrification of fatty acids |
| PL2597142T5 (en) | 2011-11-23 | 2020-10-05 | Alfa Laval Corporate Ab | De-acidification of fats and oils |
| GB2501519B (en) | 2012-04-27 | 2020-01-15 | N V Desmet Ballestra Eng Sa | Physical refining of triglyceride oils and fats |
| EP2792734B1 (en) | 2013-04-15 | 2017-07-19 | Alfa Laval Corporate AB | De-acidification of fats and oils |
| US20150342211A1 (en) * | 2014-05-28 | 2015-12-03 | Sherazi Tufail Hussain | Use of unsaponifiable extract obtained from vegetable oil deodorizer distillate for the stabilization of canola oil |
| IT201600116065A1 (en) * | 2016-11-17 | 2018-05-17 | Green Oleo Srl | PROCESS FOR THE PURIFICATION OF THE INSAPONIFIABLE FRACTION OF VEGETABLE OILS |
| US11612180B2 (en) * | 2019-03-20 | 2023-03-28 | Desmet Belgium | Versatile semi-continuous deodorizer with combined external stripping and scrubbing column |
| CN110527592A (en) * | 2019-09-27 | 2019-12-03 | 山东兴泉油脂有限公司 | The equipment and its technique of content of trans fatty acids in a kind of reduction corn oil |
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| US2349270A (en) | 1940-08-24 | 1944-05-23 | Distillation Products Inc | Purification of sludges, scums, and the like to prepare relatively purified tocopherol |
| US2410926A (en) | 1944-04-04 | 1946-11-12 | California Flaxseed Products C | Fatty oil desliming process |
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| BE905071A (en) | 1986-07-10 | 1987-01-08 | Kd Polt Inst | PROCESS FOR OBTAINING PHOSPHATIDE CONCENTRATES FROM VEGETABLE OILS. |
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| US5424457A (en) | 1994-05-27 | 1995-06-13 | Eastman Chemical Company | Process for the production of sterol and tocopherol concentrates |
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| US6172248B1 (en) | 1998-11-20 | 2001-01-09 | Ip Holdings, L.L.C. | Methods for refining vegetable oils and byproducts thereof |
| ATE312151T1 (en) * | 2001-05-14 | 2005-12-15 | Smet Engineering N V De | APPARATUS AND METHOD FOR THE PHYSICAL REFINING AND/OR DEODORIZATION OF EDIBLE OILS AND FATS |
-
2001
- 2001-09-04 US US09/946,810 patent/US6750359B1/en not_active Expired - Lifetime
-
2002
- 2002-08-27 AR ARP020103218 patent/AR038659A1/en not_active Application Discontinuation
- 2002-08-29 JP JP2003525118A patent/JP2005501908A/en not_active Abandoned
- 2002-08-29 CN CNA028186214A patent/CN1556847A/en active Pending
- 2002-08-29 WO PCT/US2002/027471 patent/WO2003020860A2/en active IP Right Grant
- 2002-08-29 BR BR0212313A patent/BR0212313A/en not_active IP Right Cessation
- 2002-08-29 DE DE60216514T patent/DE60216514D1/en not_active Expired - Lifetime
- 2002-08-29 CA CA 2459351 patent/CA2459351C/en not_active Expired - Fee Related
- 2002-08-29 EP EP02773252A patent/EP1465968B1/en not_active Expired - Fee Related
- 2002-08-29 AU AU2002336405A patent/AU2002336405A1/en not_active Abandoned
- 2002-08-29 MX MXPA04002116A patent/MXPA04002116A/en not_active Application Discontinuation
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101812373A (en) * | 2010-04-16 | 2010-08-25 | 南通市康桥油脂有限公司 | Method for producing fatty acid by continuous graded rectification |
| CN101812373B (en) * | 2010-04-16 | 2012-03-07 | 南通市康桥油脂有限公司 | Method for producing fatty acid by continuous graded rectification |
| CN103491793A (en) * | 2011-03-24 | 2014-01-01 | 荷兰洛德斯克罗科兰有限公司 | Process for fractionating a vegetable oil |
| CN102311876A (en) * | 2011-08-16 | 2012-01-11 | 山东渤海实业股份有限公司 | Two-grade distillate capture method in plant oil deodorization processing and device thereof |
| CN104508100A (en) * | 2012-07-12 | 2015-04-08 | 阿尔法拉瓦尔股份有限公司 | Deacidification of fats and oils |
| US9816047B2 (en) | 2012-07-12 | 2017-11-14 | Alfa Laval Corporate Ab | Deacidification of fats and oils |
Also Published As
| Publication number | Publication date |
|---|---|
| EP1465968B1 (en) | 2006-11-29 |
| EP1465968A4 (en) | 2005-12-14 |
| WO2003020860A3 (en) | 2004-08-05 |
| BR0212313A (en) | 2004-08-31 |
| WO2003020860A2 (en) | 2003-03-13 |
| EP1465968A2 (en) | 2004-10-13 |
| US6750359B1 (en) | 2004-06-15 |
| CA2459351C (en) | 2005-11-01 |
| DE60216514D1 (en) | 2007-01-11 |
| CA2459351A1 (en) | 2003-03-13 |
| AU2002336405A1 (en) | 2003-03-18 |
| JP2005501908A (en) | 2005-01-20 |
| AR038659A1 (en) | 2005-01-26 |
| MXPA04002116A (en) | 2004-07-08 |
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